DE69310429T3 - Process for the production of high pressure nitrogen and oxygen - Google Patents

Process for the production of high pressure nitrogen and oxygen

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Publication number
DE69310429T3
DE69310429T3 DE69310429T DE69310429T DE69310429T3 DE 69310429 T3 DE69310429 T3 DE 69310429T3 DE 69310429 T DE69310429 T DE 69310429T DE 69310429 T DE69310429 T DE 69310429T DE 69310429 T3 DE69310429 T3 DE 69310429T3
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DE
Germany
Prior art keywords
pressure
nitrogen
oxygen
column
compressor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
DE69310429T
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German (de)
Other versions
DE69310429T2 (en
DE69310429D1 (en
Inventor
Yves Koeberle
Jean-Pierre Tranier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
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Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04121—Steam turbine as the prime mechanical driver
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

Die Erfindung betrifft ein Verfahren zur gleichzeitigen Herstellung von einerseits reinem Stickstoff unter einem hohen Stickstoffdruck und andererseits Sauerstoff durch Destillation von Luft in einer Doppel-Destillationskolonne, umfassend eine Mitteldruckkolonne und eine Niederdruckkolonne nach Art eines "Minaretts", die an ihrem Kopf den reinen Stickstoff liefert.The invention relates to a process for the simultaneous production of pure nitrogen under a high nitrogen pressure and oxygen by distillation of air in a double distillation column, comprising a medium-pressure column and a low-pressure column in the form of a "minaret" which delivers pure nitrogen at its top.

Die Erfindung ist vor allem nützlich bei der gleichzeitigen Herstellung von einerseits weniger als 10 ppm Sauerstoff enthaltendem Stickstoff hoher Reinheit in großen Mengen (d. h. der Stickstoff entspricht mindestens 20% und typisch mehr als 30% des behandelten Luftstroms) unter einem Druck von 50 bis 60 bar für eine Ammoniakproduktionseinheit und andererseits Sauerstoff mittlerer bis hoher Reinheit, d. h. 95 bis 99,5 mol-%, bei einem Druck in der Größenordnung von 65 bar mit einer hohen Extraktionsausbeute zur Herstellung von Wasserstoff mittels Reaktion des Sauerstoffs mit schweren Kohlenwasserstoffen; der Wasserstoff ist zur Versorgung der selben Ammoniakproduktionseinheit bestimmt.The invention is particularly useful for the simultaneous production, on the one hand, of high purity nitrogen containing less than 10 ppm of oxygen in large quantities (i.e. the nitrogen represents at least 20% and typically more than 30% of the air stream treated) at a pressure of 50 to 60 bar for an ammonia production unit and, on the other hand, of medium to high purity oxygen, i.e. 95 to 99.5 mol%, at a pressure of the order of 65 bar with a high extraction yield for the production of hydrogen by reaction of the oxygen with heavy hydrocarbons; the hydrogen is intended to supply the same ammonia production unit.

Unter einer "Niederdruckkolonne nach Art eines Minaretts" ist eine Niederdruckkolonne zu verstehen, die ein Teil einer Luft-Doppel-Destillationskolonne ist, deren oberer Endbereich am Kopf mit am Kopf der Mitteldruckkolonne entnommener und entspannter "oberer, armer Flüssigkeit" (im wesentlichen reiner Stickstoff) gespeist wird und am Kopf Stickstoff unter dem Niederdruck liefert.A "minaret-type low-pressure column" is to be understood as meaning a low-pressure column which is part of an air-double distillation column, the upper end section of which is fed at the top with "top lean liquid" (essentially pure nitrogen) taken from the top of the medium-pressure column and expanded, and which supplies nitrogen at the top under the low pressure.

Die hier genannten Drücke sind Absolutdrücke. Zudem sind unter "Niederdruck" und "Mitteldruck" die Betriebsdrücke der Niederdruckkolonne bzw. der Mitteldruckkolonne der Doppelkolonne zu verstehen.The pressures mentioned here are absolute pressures. In addition, "low pressure" and "medium pressure" refer to the operating pressures of the low-pressure column and the medium-pressure column of the double column, respectively.

Die US-A-2 982 108 beschreibt ein Verfahren zur gleichzeitigen Herstellung von unter Druck stehendem Stickstoff und Sauerstoff, bei dem ein Verdichter das Stickstoffprodukt auf einen Druck von maximal 40 bar bringt, vorausgesetzt, der Verdichter hat höchstens vier Laufräder.US-A-2 982 108 describes a process for the simultaneous production of pressurized nitrogen and oxygen, in which a compressor brings the nitrogen product to a maximum pressure of 40 bar, provided that the compressor has a maximum of four impellers.

Die Erfindung schlägt ein Verfahren gemäß dem Anspruch 1 vor.The invention proposes a method according to claim 1.

Nach einer bevorzugten Ausführungform der Erfindung wird der Stickstoff aus dem Kreislauf auf einen unterkritischen Druck verdichtet, bei dem die Kondensationstemperatur des Stickstoffs ein wenig geringer ist als die Verdampfungstemperatur des Sauerstoffs unter dem genannten Sauerstoffzwischendruck.According to a preferred embodiment of the invention, the nitrogen from the circuit is compressed to a subcritical pressure at which the condensation temperature of the nitrogen is slightly lower than the evaporation temperature of the oxygen under the said intermediate oxygen pressure.

Nach einer anderen bevorzugten Ausführungsform der Erfindung wird zur Kühlung der Vorrichtung zur Destillation von Luft aus der Niederdruckkolonne entnommener Rohstickstoff in einer Turbine entspannt, wobei dieser Rohstickstoff nach Entspannung und Anwärmung vorzugsweise verwendet wird, um Adsorptionsflaschen, die der Reinigung der behandelten Luft dienen, zu regenerieren.According to another preferred embodiment of the invention, raw nitrogen taken from the low-pressure column is expanded in a turbine to cool the device for distilling air, and this raw nitrogen, after expansion and heating, is preferably used to regenerate adsorption bottles which serve to purify the treated air.

Der Stickstoffverdichter und der Luftverdichter können insbesondere mit einem gemeinsamen motorischen Antrieb verbunden sein.The nitrogen compressor and the air compressor can be connected, in particular, to a common motor drive.

Ein Ausführungsbeispiel nach der Erfindung wird nun anhand der Zeichnung beschrieben; die einzige Figur zeigt schematisch eine Vorrichtung zur gleichzeitigen Herstellung von Sauerstoff und Stickstoff unter hohem Druck zur Durchführung eines Verfahrens nach der Erfindung.An embodiment according to the invention will now be described with reference to the drawing; the single figure shows schematically an apparatus for the simultaneous production of oxygen and nitrogen under high pressure for carrying out a method according to the invention.

Die in der Zeichnung dargestellte Vorrichtung ist zur Herstellung von einerseits gasförmigem Stickstoff mit hoher Reinheit (mit typischerweise weniger als 10 ppm Sauerstoff) unter einem Druck von 55 bar mit einer Ausbeute entsprechend mindestens 20% des behandelten Luftstroms und andererseits Sauerstoff mit einer Reinheit von 95 bis 99,5% unter einem Druck von 65 bar mit einer erhöhten Extraktionsausbeute. Die zwei unter Hochdruck stehenden Gase werden an der selben Stelle verwendet: Wasserstoff wird mittels Reaktion von Sauerstoff mit schweren Kohlenwasserstoffen hergestellt und danach reagieren dieser Wasserstoff und Stickstoff zur Herstellung von Ammoniak.The device shown in the drawing is designed to produce, on the one hand, gaseous nitrogen with high purity (typically less than 10 ppm oxygen) under a pressure of 55 bar with a yield corresponding to at least 20% of the treated air flow and, on the other hand, oxygen with a purity of 95 to 99.5% under a pressure of 65 bar with an increased extraction yield. The two high pressure gases are used at the same point: hydrogen is produced by reacting oxygen with heavy hydrocarbons and then this hydrogen and nitrogen react to produce ammonia.

Die Vorrichtung umfaßt im wesentlichen einen Luftverdichter 1, eine Vorrichtung 2 zur Reinigung von Luft mittels Adsorption, eine Wärmeaustauschleitung 3 vom Gegenstromtyp, eine Doppel-Destillationskolonne 4, eine Entspannungsturbine 5, eine Pumpe für flüssigen Sauerstoff 6, einen Stickstoffverdichter 7, einen Sauerstoffverdichter 8 und eine Energiequelle 9, die z. B. eine Dampfturbine ist.The device essentially comprises an air compressor 1, a device 2 for purifying air by means of adsorption, a heat exchange line 3 of the countercurrent type, a double distillation column 4, an expansion turbine 5, a liquid oxygen pump 6, a nitrogen compressor 7, an oxygen compressor 8 and an energy source 9, which is, for example, a steam turbine.

Die Doppelkolonne 4 umfaßt eine auf einer Niederdruckkolonne 11 angeordnete Mitteldruckkolonne 10, deren oberer Endbereich ein Minarett 11A zur Herstellung von reinem Sauerstoff unter dem Niederdruck bildet. Ein Kondensator-Verdampfer 12 stellt den Wärmeaustausch zwischen dem Kopfdampf (im wesentlichen reiner Stickstoff) der Kolonne 10 und der Sumpfflüssigkeit (Sauerstoff mit festgelegter Reinheit) der Kolonne 11 her. Wie üblich ermöglicht eine mit einem Druckminderventil 13 ausgestattete Leitung die "reiche Flüssigkeit" (sauerstoffangereicherte Luft) aus dem Sumpf der Kolonne 10 zu einem Zwischenpunkt der Kolonne 11 zurückzuführen; eine mit einem Druckminderventil 14 ausgestattete Leitung ermöglicht, die "untere arme Flüssigkeit" (Rohstickstoff) von einem Zwischenpunkt der Kolonne 10 zu der Basis des Minaretts 11A zurückzuführen; und eine mit einem Druckminderventil 15 ausgestattete Leitung ermöglicht, die "obere arme Flüssigkeit" (im wesentlichen reiner Stickstoff) vom Kopf der Kolonne 10 zu der Spitze des Minaretts zurückzuführen.The double column 4 comprises a medium pressure column 10 arranged on a low pressure column 11, the upper end of which forms a minaret 11A for producing pure oxygen under the low pressure. A condenser-evaporator 12 provides the heat exchange between the top vapor (essentially pure nitrogen) of the column 10 and the bottom liquid (oxygen of a fixed purity) of the column 11. As usual, a line equipped with a pressure reducing valve 13 allows the "rich liquid" (oxygen-enriched air) from the bottom of the column 10 to be returned to an intermediate point of the column 11; a line equipped with a pressure reducing valve 14 allows the "lower poor liquid" (crude nitrogen) from an intermediate point of the column 10 to the base of the minaret 11A; and a line equipped with a pressure reducing valve 15 enables the "upper poor liquid" (essentially pure nitrogen) to be returned from the top of the column 10 to the top of the minaret.

Der Stickstoffverdichter 7 ist aus einem einzigen, dreistufigen Verdichter aufgebaut. Die zwei ersten Stufen umfassen jeweils zwei Verdichterräder und haben mittlere Verdichtungsverhältnisse pro Rad von 2 bzw. 1,73, während die dritte Stufe ein einziges Verdichterrad mit einem Verdichtungsverhältnis von 1,83 umfaßt. Das Gesamtverdichtungsverhältnis des Verdichters ist daher 22. Jedes Rad hat an seinem Auslaß ein Kühlmittel.The nitrogen compressor 7 is constructed from a single, three-stage compressor. The first two stages each comprise two compressor wheels and have average compression ratios per wheel of 2 and 1.73 respectively, while the third stage comprises a single compressor wheel with a compression ratio of 1.83. The overall compression ratio of the compressor is therefore 22. Each wheel has a coolant at its outlet.

Der Sauerstoffverdichter 8 besteht ebenfalls aus einem einzigen Verdichter. Dieser Verdichter hat sechs Räder mit einem mittlerem Verdichtungsverhältnis pro Rad von 1,37. Das Gesamtverdichtungsverhältnis ist daher 6,5.The oxygen compressor 8 also consists of a single compressor. This compressor has six wheels with an average compression ratio per wheel of 1.37. The total compression ratio is therefore 6.5.

Die Welle 16 der Verdichters 7 ist mit der Welle 17 des Verdichters 1 mittels einer Kupplung 18 verbunden und die Anordnung wird durch eine gemeinsame Energiequelle 9 angetrieben. Gegebenenfalls kann die Welle 16 die verschiedenen Stufen des Verdichters 7 über jeder Stufe angepaßter Übersetzungsgetriebe antreiben. Der Verdichter 8 wird mittels einer eigenen Energiequelle 19 angetrieben.The shaft 16 of the compressor 7 is connected to the shaft 17 of the compressor 1 by means of a coupling 18 and the arrangement is driven by a common energy source 9. If necessary, the shaft 16 can drive the various stages of the compressor 7 via transmission gears adapted to each stage. The compressor 8 is driven by means of its own energy source 19.

Der Niederdruck wird so gewählt, daß er, multipliziert mit dem Verdichtungsverhältnis des Verdichters 7, den für Stickstoff gewünschten Produktionshochdruck liefert. Daraus ergibt sich bei Vernachlässigung der Druckverluste für einen Stickstoffhochdruck von 55 bar ein Niederdruck von 55/22 = 2,5 bar. Für einen Temperaturunterschied von 2ºC in dem Verdampfer-Kondensator 12 entspricht dies einem Mitteldruck in der Größenordnung von 11 bar.The low pressure is selected so that, multiplied by the compression ratio of the compressor 7, it delivers the high production pressure required for nitrogen. Neglecting the pressure losses, this results in a low pressure of 55/22 = 2.5 bar for a high nitrogen pressure of 55 bar. For a temperature difference of 2ºC in the evaporator-condenser 12, this corresponds to a medium pressure in the order of 11 bar.

Die eintretende Luft wird somit in dem Verdichter 1 auf 11 bar verdichtet, in 2 gereinigt, von dem warmen Ende zum kalten Ende der Wärmeaustauschleitung 3 gekühlt und nahe ihrem Taupunkt in den Sumpf der Kolonne 10 eingeleitet. Der reine Niederdruckstickstoff, der gasförmig an der Spitze des Minaretts 11A austritt und vom kalten Ende zum warmen Ende der Wärmeaustauschleitung erwärmt wird, wird über eine Leitung 23 dem Einlaß der zweiten Stufe des Verdichter 7 zugeführt. Der unter dem hohen Druck des Kreislaufes stehende Stickstoff wird am Auslaß der zweiten Stufe über eine Leitung 24 entnommen, gekühlt, verflüssigt, in der Wärmeaustauschleitung unterkühlt, in einem Druckminderventil 25 auf den Mitteldruck entspannt und in den Kopf der Kolonne 10 eingeleitet.The incoming air is thus compressed to 11 bar in the compressor 1, cleaned in 2, cooled from the warm end to the cold end of the heat exchange line 3 and introduced into the bottom of the column 10 near its dew point. The pure low-pressure nitrogen, which exits in gaseous form at the top of the minaret 11A and is heated from the cold end to the warm end of the heat exchange line, is fed to the inlet of the second stage of the compressor 7 via a line 23. The nitrogen under the high pressure of the circuit is removed at the outlet of the second stage via a line 24, cooled, liquefied, subcooled in the heat exchange line, expanded to the medium pressure in a pressure reducing valve 25 and introduced into the top of the column 10.

Infolge nicht dargestellter Durchflußregler ist der in der Leitung 24 fließende Stickstoffstrom größer als eine vorbestimmte Menge eines in der Leitung 23 fließenden Stickstoffstroms. Der Unterschied besteht in einem zusätzlichen, flüssigen Stickstoffstrom, genannt Rektifikationsunterstützung, der als Rückfluß in den Kopf der Kolonne 10 eingeleitet wird. Dieser Strom wird dem Niederdruckstickstoffstrom zugegeben, der von der ersten Stufe des Verdichters 7 angesaugt wird.Due to flow regulators not shown, the nitrogen flow in line 24 is greater than a predetermined amount of a nitrogen flow in line 23. The difference is an additional liquid nitrogen flow, called rectification support, which is introduced as reflux into the top of column 10. This flow is added to the low pressure nitrogen flow which is drawn in from the first stage of compressor 7.

Rohstickstoff, der das Restgas der Vorrichtung bildet, wird an der Basis des Minaretts 11A über eine Leitung 25 entnommen, in der Wärmeaustauschleitung auf eine Zwischentemperatur erwärmt, dieser entnommen, in einer die Kühlung der Vorrichtung gewährleistenden Turbine 5 auf Atmosphärendruck entspannt, dann in die Austauschleitung 4 eingeleitet, auf Umgebungstemperatur erwärmt, schließlich zur Regeneration der Adsorptionsflaschen 2 der Einrichtung verwendet und der Vorrichtung über eine Leitung 26 entnommen.Raw nitrogen, which constitutes the residual gas of the device, is taken from the base of the minaret 11A via a line 25, heated to an intermediate temperature in the heat exchange line, taken from this, expanded to atmospheric pressure in a turbine 5 ensuring the cooling of the device, then introduced into the exchange line 4, heated to ambient temperature, finally used to regenerate the adsorption bottles 2 of the device and taken from the device via a line 26.

Der unter einem Druck von 65 bar stehende Sauerstoff wird auf folgende Weise hergestellt.The oxygen under a pressure of 65 bar is produced in the following way.

Der gewünschte, flüssige Sauerstoffstrom wird dem Sumpf der Kolonne 11 entnommen, mit der Pumpe 6 auf einen Sauerstoffzwischendruck gebracht, verdampft und in der Wärmeaustauschleitung 3 auf Umgebungstemperatur erwärmt, und anschließend mit dem Verdichter 8 auf den Produktionsdruck verdichtet.The desired liquid oxygen stream is taken from the bottom of the column 11, brought to an intermediate oxygen pressure using the pump 6, evaporated and heated to ambient temperature in the heat exchange line 3, and then compressed to the production pressure using the compressor 8.

Um die thermodynamischen Irreversibilitäten in der Wärmeaustauschleitung bestmöglich zu begrenzen, wird die Verdampfung des unter dem Säuerstoffzwischendruck stehenden flüssigen Sauerstoffs mittels Kondensation des unter dem Kreishochdruck stehenden Stickstoffs bei einem unterkritischen Wert dieses Hochdrucks, d. h. beispielsweise bei 30 bar, durchgeführt. Dieser Wert entspricht einer Verdampfung von flüssigem Sauerstoff unter einem Druck von ungefähr 11 bar, der daher der Druck ist, der von der Pumpe 6 geliefert wird.In order to limit the thermodynamic irreversibilities in the heat exchange line as much as possible, the evaporation of the liquid oxygen at the intermediate oxygen pressure is carried out by condensing the nitrogen at the high pressure of the circuit at a subcritical value of this high pressure, i.e. for example at 30 bar. This value corresponds to an evaporation of liquid oxygen at a pressure of approximately 11 bar, which is therefore the pressure supplied by the pump 6.

Unter Berücksichtigung des obigen ergeben sich folgende Drücke für die verschiedenen Stufen des Verdichters 7: 2,5 bar am Einlaß der ersten Stufe, 11 bar am Einlaß der zweiten Stufe, 30 bar am Einlaß der dritten Stufe und 55 bar am Auslaß dieser dritten Stufe.Taking the above into account, the following pressures result for the various stages of compressor 7: 2.5 bar at the inlet of the first stage, 11 bar at the inlet of the second stage, 30 bar at the inlet of the third stage and 55 bar at the outlet of this third stage.

Es läßt sich zeigen, daß das oben beschriebene Verfahren im Vergleich zu dem klassischen Verfahren, bei dem der Produktionsstickstoffstrom mindestens 20% des behandelten Luftstroms ist, einen Investitionsvorteil liefert, sobald der Niederdruck ein wenig oberhalb von 1 bar gewählt wird. Wenn die Stickstoffproduktion größer als ungefähr 30% des Luftstroms ist, liefert es zu dem einen Energiegewinn. Des weiteren ist das Reinigen der unter einem Druck von 11 bar eintretenden Luft aus ökonomischer Sicht sehr vorteilhaft.It can be shown that the process described above provides an investment advantage when compared to the classic process, in which the production nitrogen flow is at least 20% of the treated air flow, as long as the low pressure is chosen a little above 1 bar. When the nitrogen production is greater than about 30% of the air flow, it also provides an energy gain. Furthermore, cleaning the air entering at a pressure of 11 bar is very advantageous from an economic point of view.

Claims (3)

1. Verfahren zur gleichzeitigen Herstellung von einerseits reinem Stickstoff unter einem hohen Stickstoffdruck von 50 bis 60 bar und andererseits Sauerstoff durch Destillation von Luft in einer Doppel-Destillationskolonne (4), umfassend eine Mitteldruckkolonne (10) und eine Niederdruckkolonne (11) nach Art eines "Minaretts", die an ihrem Kopf den reinen Stickstoff liefert, wobei der aus der Niederdruckkolonne (11) austretende Stickstoff nach Erwärmen mittels eines einzigen Stickstoffverdichters (7) des Zentrifugentyps mit höchstens sechs Verdichterrädern auf den hohen Druck verdichtet wird, wobei die Niederdruckkolonne (11) unter einem Druck in der Größenordnung von PN/ρN betrieben wird, wobei PN der hohe Stickstoffdruck und ρN das Verdichtungsverhältnis des genannten Stickstoffverdichters ist, und wobei der Sauerstoff unter einem hohen Sauerstoffdruck von mehr als etwa 10 bar absolut erzeugt wird, am Sumpf der Niederdruckkolonne (11) entnommener flüssiger Sauerstoff mit einer Pumpe (6) auf einen Sauerstoffzwischendruck gebracht und nach Verdampfen und Erwärmen mittels eines einzigen Sauerstoffverdichters (8) des Zentrifugentyps mit höchstens sechs Verdichtungsrädern auf den hohen Sauerstoffdruck verdichtet wird, wobei der Sauerstoffzwischendruck in der Größenordnung von P&sub0;/ρ&sub0; liegt, wobei P&sub0; das Verdichtungsverhältnis des genannten Sauerstoffverdichters ist und der einzige dreistufige Stickstoffverdichter (7) mit höchstens zwei Rädern pro Stufe verwendet wird und außerdem die zweite Stufe verwendet wird, um eine Menge Stickstoff aus dem Kreislauf, der aus der Mitteldruckkolonne (10) entnommen und erwärmt wurde, auf einen Zwischendruck zwischen dem mittleren Druck und dem hohen Druck zu verdichten, und der verdichtete Stickstoff aus dem Kreislauf abgekühlt, verflüssigt, auf den mittleren Druck entspannt und am Kopf der Mitteldruckkolonne (10) eingeleitet wird, und außerdem die beiden ersten Stufen verwendet werden, um zur Rektifikationsunterstützung einen Stickstoffstrom, der am Kopf der Niederdruckkolonne (11) entnommen und erwärmt wurde, von dem niedrigen Druck auf einen Zwischendruck zwischen dem mittleren Druck und dem hohen Druck zu verdichten, und dieser verdichtete Stickstoff abgekühlt, verflüssigt, auf den mittleren Druck entspannt und am Kopf der Mitteldruckkolonne (10) eingeleitet wird.1. Process for the simultaneous production of pure nitrogen under a high nitrogen pressure of 50 to 60 bar and oxygen by distillation of air in a double distillation column (4) comprising a medium pressure column (10) and a low pressure column (11) of the "minaret" type which supplies pure nitrogen at its top, the nitrogen emerging from the low pressure column (11) being compressed to the high pressure after heating by means of a single nitrogen compressor (7) of the centrifuge type with a maximum of six compressor wheels, the low pressure column (11) being operated at a pressure of the order of PN/ρN, PN being the high nitrogen pressure and ρN being the compression ratio of said nitrogen compressor, and the oxygen being produced under a high oxygen pressure of more than about 10 bar absolute, liquid oxygen taken from the bottom of the low pressure column (11) being pumped to a oxygen intermediate pressure and, after evaporation and heating, is compressed to the high oxygen pressure by means of a single centrifuge-type oxygen compressor (8) with a maximum of six compression wheels, the oxygen intermediate pressure being of the order of P₀/ρ₀, P₀ being the compression ratio of said oxygen compressor, and the single three-stage nitrogen compressor (7) with a maximum of two wheels per stage is used, and in addition the second stage is used to compress a quantity of nitrogen from the circuit taken from the medium pressure column (10) and heated to an intermediate pressure between the medium pressure and the high pressure, and the compressed nitrogen from the circuit is cooled, liquefied, expanded to the medium pressure and introduced at the top of the medium pressure column (10), and in addition the first two stages are used to compress a nitrogen stream which was taken from the top of the low pressure column (11) and heated from the low pressure to an intermediate pressure between the medium pressure and the high pressure to assist rectification, and this compressed nitrogen is cooled, liquefied, expanded to the medium pressure and introduced at the top of the medium pressure column (10). 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der Stickstoff aus dem Kreislauf auf einen unterkritischen Druck verdichtet wird, bei dem die Kondensationstemperatur des Stickstoffs ein wenig geringer ist als die Verdampfungstemperatur des Sauerstoffs unter dem genannten Sauerstoffzwischendruck.2. Process according to claim 1, characterized in that the nitrogen from the circuit is compressed to a subcritical pressure at which the condensation temperature of the nitrogen is slightly lower than the evaporation temperature of the oxygen under the said intermediate oxygen pressure. 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß zur Kühlung der Vorrichtung zur Destillation von Luft aus der Niederdruckkolonne (11) entnommener Rohstickstoff in einer Turbine (5) entspannt wird, wobei dieser Rohstickstoff nach Entspannung und Erwärmung vorzugswiese verwendet wird, um Adsorptionsflaschen (2), die der Reinigung der behandelten Luft dienen, zu regenerieren.3. Process according to claim 1 or 2, characterized in that, in order to cool the device for distilling air, raw nitrogen taken from the low-pressure column (11) is expanded in a turbine (5), whereby this raw nitrogen, after expansion and heating, is preferably used to regenerate adsorption bottles (2) which serve to purify the treated air.
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Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2703140B1 (en) * 1993-03-23 1995-05-19 Air Liquide Method and installation for producing gaseous oxygen and / or nitrogen gas under pressure by air distillation.
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
FR2706595B1 (en) * 1993-06-18 1995-08-18 Air Liquide Process and installation for producing oxygen and / or nitrogen under pressure with variable flow rate.
US5460003A (en) * 1994-06-14 1995-10-24 Praxair Technology, Inc. Expansion turbine for cryogenic rectification system
US5689975A (en) * 1995-10-11 1997-11-25 The Boc Group Plc Air separation
US5600970A (en) * 1995-12-19 1997-02-11 Praxair Technology, Inc. Cryogenic rectification system with nitrogen turboexpander heat pump
GB9618576D0 (en) * 1996-09-05 1996-10-16 Boc Group Plc Air separation
GB9618577D0 (en) * 1996-09-05 1996-10-16 Boc Group Plc Air separation
GB9619717D0 (en) * 1996-09-20 1996-11-06 Boc Group Plc Air separation
GB9619718D0 (en) * 1996-09-20 1996-11-06 Boc Group Plc Air separation
US5682762A (en) * 1996-10-01 1997-11-04 Air Products And Chemicals, Inc. Process to produce high pressure nitrogen using a high pressure column and one or more lower pressure columns
GB9810587D0 (en) * 1998-05-15 1998-07-15 Cryostar France Sa Pump
FR2782787B1 (en) 1998-08-28 2000-09-29 Air Liquide PROCESS AND PLANT FOR PRODUCING IMPURED OXYGEN BY AIR DISTILLATION
GB9903908D0 (en) * 1999-02-19 1999-04-14 Boc Group Plc Air separation
US6192707B1 (en) * 1999-11-12 2001-02-27 Praxair Technology, Inc. Cryogenic system for producing enriched air
GB0002084D0 (en) * 2000-01-28 2000-03-22 Boc Group Plc Air separation method
DE10013075A1 (en) * 2000-03-17 2001-09-20 Linde Ag Process for recovering gaseous nitrogen by the decomposition of air in a distillation column system comprises removing a part of the nitrogen-rich liquid from the condenser-vaporizer as a liquid product
EP1202012B1 (en) 2000-10-30 2005-12-07 L'AIR LIQUIDE, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Process and installation for cryogenic air separation integrated with an associated process
WO2003016676A1 (en) 2001-08-15 2003-02-27 Shell Internationale Research Maatschappij B.V. Tertiary oil recovery combined with gas conversion process
WO2005044954A1 (en) * 2003-10-29 2005-05-19 Shell Internationale Research Maatschappij B.V. Process to transport a methanol or hydrocarbon product
FR2863348B1 (en) * 2003-12-05 2006-12-22 Air Liquide GAS COMPRESSOR, APPARATUS FOR SEPARATING A GAS MIXTURE INCORPORATING SUCH A COMPRESSOR, AND METHOD FOR SEPARATING A GAS MIXTURE INCORPORATING SUCH A COMPRESSOR
US7225637B2 (en) * 2004-12-27 2007-06-05 L'Air Liquide Société Anonyme á´ Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Integrated air compression, cooling, and purification unit and process
US7712331B2 (en) * 2006-06-30 2010-05-11 Air Products And Chemicals, Inc. System to increase capacity of LNG-based liquefier in air separation process
DE102010056570A1 (en) 2010-12-30 2012-07-05 Linde Aktiengesellschaft Method for obtaining pressure of oxygen and nitrogen by low-temperature fractionation of air, involves performing stress-free compressing process in distillation column system for initiating nitrogen-oxygen separation
EP2963367A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for cryogenic air separation with variable power consumption
EP3059536A1 (en) * 2015-02-19 2016-08-24 Linde Aktiengesellschaft Method and device for obtaining a pressurised nitrogen product
KR20220166824A (en) * 2020-04-09 2022-12-19 린데 게엠베하 An integrated system consisting of a cryogenic classification process of air, an air classification plant and at least two air classification plants

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1138601A (en) * 1955-12-15 1957-06-17 Air Liquide Improvements in the purification and separation of air into its elements
DE1112997B (en) * 1960-08-13 1961-08-24 Linde Eismasch Ag Process and device for gas separation by rectification at low temperature
US3123457A (en) * 1960-12-22 1964-03-03 E smith
DE1263037B (en) * 1965-05-19 1968-03-14 Linde Ag Method for the separation of air in a rectification column and the separation of a gas mixture containing hydrogen
SU739316A1 (en) † 1977-08-22 1980-06-05 Предприятие П/Я А-3605 Method of segregating air
GB2079428A (en) * 1980-06-17 1982-01-20 Air Prod & Chem A method for producing gaseous oxygen
US4869741A (en) * 1988-05-13 1989-09-26 Air Products And Chemicals, Inc. Ultra pure liquid oxygen cycle
EP0383994A3 (en) † 1989-02-23 1990-11-07 Linde Aktiengesellschaft Air rectification process and apparatus

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